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US9688591B2 - Ethylene separation process - Google Patents

Ethylene separation process Download PDF

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Publication number
US9688591B2
US9688591B2 US13/738,685 US201313738685A US9688591B2 US 9688591 B2 US9688591 B2 US 9688591B2 US 201313738685 A US201313738685 A US 201313738685A US 9688591 B2 US9688591 B2 US 9688591B2
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US
United States
Prior art keywords
ethylene
stream
ethenizer
metathesis
butene
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Application number
US13/738,685
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English (en)
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US20140194664A1 (en
Inventor
Gary A. Sawyer
Robert S. Bridges
Steven T. Coleman
Allen David Hood, JR.
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Lyondell Chemical Technology LP
Equistar Chemicals LP
Original Assignee
Lyondell Chemical Technology LP
Equistar Chemicals LP
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
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Publication date
Application filed by Lyondell Chemical Technology LP, Equistar Chemicals LP filed Critical Lyondell Chemical Technology LP
Assigned to EQUISTAR CHEMICALS, LP reassignment EQUISTAR CHEMICALS, LP ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: COLEMAN, STEVEN T, HOOD, ALLEN DAVID, JR
Priority to US13/738,685 priority Critical patent/US9688591B2/en
Assigned to LYONDELL CHEMICAL TECHNOLOGY, L.P. reassignment LYONDELL CHEMICAL TECHNOLOGY, L.P. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: SAWYER, GARY A, BRIDGES, ROBERT S
Priority to SG11201504150RA priority patent/SG11201504150RA/en
Priority to MYPI2015701766A priority patent/MY170494A/en
Priority to BR112015015460-3A priority patent/BR112015015460B1/pt
Priority to EP14738270.9A priority patent/EP2943453B1/fr
Priority to MX2015008359A priority patent/MX364862B/es
Priority to CA2896614A priority patent/CA2896614C/fr
Priority to CN201480003719.9A priority patent/CN104918903A/zh
Priority to PCT/US2014/010631 priority patent/WO2014110102A1/fr
Priority to RU2015130732A priority patent/RU2609014C2/ru
Priority to KR1020157020376A priority patent/KR101791760B1/ko
Publication of US20140194664A1 publication Critical patent/US20140194664A1/en
Priority to SA515360681A priority patent/SA515360681B1/ar
Publication of US9688591B2 publication Critical patent/US9688591B2/en
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/04—Purification; Separation; Use of additives by distillation
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C11/00—Aliphatic unsaturated hydrocarbons
    • C07C11/02—Alkenes
    • C07C11/04—Ethylene
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C11/00—Aliphatic unsaturated hydrocarbons
    • C07C11/02—Alkenes
    • C07C11/06—Propene
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C4/00—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
    • C07C4/02—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by cracking a single hydrocarbon or a mixture of individually defined hydrocarbons or a normally gaseous hydrocarbon fraction
    • C07C4/06—Catalytic processes
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C6/00—Preparation of hydrocarbons from hydrocarbons containing a different number of carbon atoms by redistribution reactions
    • C07C6/02—Metathesis reactions at an unsaturated carbon-to-carbon bond
    • C07C6/04—Metathesis reactions at an unsaturated carbon-to-carbon bond at a carbon-to-carbon double bond

Definitions

  • the present invention generally relates to ethylene separation processes. More particularly, the present invention generally relates to ethylene separation within a propylene production process.
  • Ethylene separation processes within propylene production processes often exchange fresh ethylene with the feed to the ethylene separation process prior to introduction of the fresh ethylene to a metathesis reaction.
  • efforts are continuously underway to improve ethylene separation processes, including reducing energy requirements and other costs in propylene production processes.
  • the present invention is directed to resolving, or at least reducing, one or all of the problems mentioned above.
  • Various embodiments of the present invention include ethylene en e separation processes.
  • the ethylene separation processes generally include introducing a feed stream including ethylene and butene into a de-ethenizer; and separating the ethylene from the butene via fractional distillation within the de-ethenizer to form an overhead stream including separated ethylene and a bottoms stream including separated butene, wherein the de-ethenizer operates at a pressure of less than 350 psig.
  • Various embodiments of the present invention further include processes for producing propylene.
  • the processes generally include reacting a metathesis feed stream including butene with ethylene in the presence of a metathesis catalyst via a metathesis reaction to form a metathesis product stream including propylene, ethylene and butene; separating the ethylene from the propylene via fractional distillation within a de-ethenizer to form an overhead stream including separated ethylene and a bottoms stream including separated butene and propylene; and recycling the overhead stream from the de-ethenizer to the metathesis reaction in the form of vapor.
  • One or more embodiments include the process of any preceding paragraph further including compressing the overhead stream from a first pressure to a second pressure.
  • One or more embodiments include the process of any preceding paragraph, wherein the first pressure ranges from 250 psig to 325 psig and the second pressure ranges from 300 psig to 400 psig.
  • One or more embodiments include the process of any preceding paragraph, wherein a difference between the second pressure and the first pressure is from 50 psig to 100 psig.
  • One or more embodiments include the process of any preceding paragraph further including condensing a portion of the overhead stream to form a recycle ethylene stream and introducing the recycle ethylene stream to the de-ethenizer, wherein the overhead stream is compressed prior to condensing.
  • One or more embodiments include the process of any preceding paragraph, further including introducing fresh ethylene to the de-ethenizer as reflux supplement.
  • One or more embodiments include the process of any preceding paragraph, wherein the de-ethenizer operates at a pressure of less than 350 psig.
  • One or more embodiments include the process of any preceding paragraph, wherein the feed stream further including propylene.
  • One or more embodiments include the process of any preceding paragraph further including condensing a portion of the overhead stream to form a recycle ethylene stream and introducing the recycle ethylene stream to the de-ethenizer.
  • One or more embodiments include the process of any preceding paragraph, wherein the fresh ethylene is introduced to the de-ethenizer at a temperature of from ⁇ 20° F. to 10° F.
  • One or more embodiments include the process of any preceding paragraph, wherein the metathesis product stream is introduced to the de-ethenizer at a temperature of from 50° F. to 90° F.
  • One or more embodiments include the process of any preceding paragraph, wherein the metathesis product stream is introduced to the de-ethenizer at a pressure of from 250 psig to 350 psig.
  • FIG. 1 illustrates an embodiment of a propylene production process.
  • FIG. 2 illustrates an alternate embodiment of a propylene production process.
  • Embodiments described herein include ethylene separation processes.
  • the ethylene separation processes are discussed primarily herein with reference to separating a metathesis product stream within a propylene production process. However, it is contemplated that the ethylene separation processes described herein may be utilized within any process requiring separation of ethylene from butene.
  • Propylene production processes generally includes reacting a metathesis feed stream including n-butene with ethylene in the presence of a metathesis catalyst to form a metathesis product stream including propylene, ethylene, butene and C 5+ olefins.
  • a metathesis refers to an equilibrium reaction between two olefins where the double bond of each olefin is broken to form intermediate reactants. These intermediates recombine to form new olefin products.
  • the two olefins include ethylene and butene and the new olefin product is propylene.
  • n-butene is fed to the metathesis reaction via the metathesis feed stream.
  • the ethylene may be fed to the reaction by any suitable method known to one skilled in the art.
  • the ethylene may be fed to the metathesis reaction via an inlet separate from an inlet utilized to feed the metathesis feed stream.
  • the ethylene may be combined with the metathesis feed stream prior to the metathesis feed stream passing through such inlet.
  • Metathesis catalysts are well known in the art (see, e.g., U.S. Pat. No. 4,513,099 and U.S. Pat. No. 5,120,894).
  • the metathesis catalyst includes a transition metal oxide, such as transition metal oxides of cobalt, molybdenum, rhenium, tungsten and combinations thereof, for example.
  • the metathesis catalyst includes tungsten oxide.
  • the metathesis catalyst may be supported on a carrier, such as silica, alumina, titania, zirconia, zeolites, clays and mixtures thereof, for example.
  • the carrier is selected from silica, alumina and combinations thereof.
  • the catalyst may be supported on a carrier by methods known in the art, such as adsorption, ion-exchange, impregnation or sublimation, for example.
  • the metathesis catalyst may include from 1 wt. % to 30 wt. % or from 5 wt. % to 20 wt. % transition metal oxide, for example.
  • the metathesis reaction may further include contacting the butene with ethylene in the presence of an isomerization catalyst (either sequentially or simultaneously with the metathesis catalyst).
  • the isomerization catalyst is generally adapted to convert 1-butene present in the metathesis feed stream to 2-butene for subsequent reaction to propylene.
  • Isomerization catalysts may include zeolites, metal oxides (e.g., magnesium oxide, tungsten oxide, calcium oxide, barium oxide, lithium oxide and combinations thereof), mixed metal oxides (e.g., silica-alumina, zirconia-silica), acidic clays (see, e.g., U.S. Pat. No. 5,153,165; U.S. Pat. No. 4,992,613; U.S.
  • the catalyst is magnesium oxide.
  • the magnesium oxide may have a surface area of at least 1 m 2 /g or at least 5 m 2 /g, for example.
  • the isomerization catalyst may be supported on a support material.
  • Suitable support materials include silica, alumina, titania, silica-alumina and combinations thereof, for example.
  • the metathesis reaction may occur at a pressure of from 150 psig to 600 psig, or from 200 psig to 500 psig, or from 240 psig to 450 psig, for example.
  • the metathesis reactions may occur at a temperature of from 100° C. to 500° C., or from 200° C. to 400° C., or from 300° C. to 350° C., for example.
  • the methathesis reaction may occur at a weight hourly space velocity (WHSV) of from 3 hr ⁇ 1 to 200 hr ⁇ 1 , or from 20 hr ⁇ 1 to 40 hr ⁇ 1 , for example.
  • WHSV weight hourly space velocity
  • the contact time needed to obtain a desirable yield of metathesis reaction products depends upon several factors, such as the activity of the catalyst, temperature and pressure, for example. However, in one or more embodiments, the length of time during which the metathesis feed stream and the ethylene are contacted with the catalyst can vary from 0.1 s to 4 hours or from 0.5 s to 0.5 hours, for example.
  • the metathesis reaction may be conducted batch-wise or continuously with fixed catalyst beds, slurried catalyst, fluidized beds, or by using any other conventional contacting techniques, for example.
  • the metathesis product stream generally includes ethylene, propylene, C 4 olefins, and C 5+ olefins (including pentene and hexene, for example). Therefore, the propylene production process often includes separating the components of the metathesis product stream.
  • An example of a method of separation is shown in U.S. Pat. No. 7,214,841, which is hereby incorporated by reference, and such method generally includes separation within a fractionation system.
  • the term “fractionation” refers to processes for the separation of components based on the relative volatility and/or boiling point of the components.
  • the fractionation processes may include those known in the art and the term “fractionation” can be used interchangeably with the terms “distillation” and “fractional distillation” herein.
  • the fractionation system generally includes a de-ethenizer.
  • the de-ethenizer receives and separates the metathesis product stream to form an overhead stream and a bottoms stream.
  • the overhead stream is composed primarily of the recovered ethylene and at least a portion of the overhead stream may be recycled back to the metathesis reaction (discussed in further detail below).
  • the bottoms stream generally includes the propylene, butene and C 5+ olefins.
  • Reflux is a distillation technique involving the condensation of vapors and the return of this condensate to the system from which it originated.
  • the downflowing reflux liquid provides cooling and condensation of the upflowing vapors, thereby increasing the efficiency of the distillation column.
  • the reflux liquid is the portion of the overhead stream from a distillation column that is returned to the upper part of the column.
  • the entire de-ethenizer overhead stream is condensed to form a condensed stream, which may then be split into a reflux liquid stream and a recycle ethylene stream. In such processes, the recycle ethylene stream is returned to the metathesis reaction in liquid form.
  • One or more embodiments include partially condensing the overhead stream to form a reflux liquid stream and a recycle ethylene stream, which may then be returned to the metathesis reaction in vapor form.
  • the overhead stream may be recycled (i.e., returned to the metathesis reaction) without passing through a condenser.
  • the ethylene vapor may be compressed via a compressor from a first pressure to a second pressure sufficient to provide flow of the ethylene vapor to the metathesis reaction.
  • the first pressure may range from 250 psig to 325 psig and the second pressure may range from 300 psig to 400 psig, for example.
  • the difference in the first pressure and the second pressure may be from 50 psig to 100 psig, for example.
  • One specific embodiment includes compressing the overhead product to raise the condensing temperature utilized in a subsequent partial condenser.
  • One or more embodiments include introducing fresh ethylene to the upper portion of the de-ethenizer, either in addition to, or as a replacement for the reflux liquid stream. Accordingly, the fresh ethylene introduced to the de-ethenizer is referred to as reflux supplement herein. As known in the art, “fresh” ethylene refers to ethylene that has not been processed in the system being referred to, herein the propylene production process. In one or more embodiments, the fresh ethylene is introduced to the de-ethenizer as reflux supplement at a rate that is less than that of the reflux liquid stream.
  • the fresh ethylene/reflux supplement is introduced to the de-ethenizer at a temperature of from ⁇ 20° F. to 100° F., or from ⁇ 10° F. to 50° F., or from ⁇ 10° F. to 10° F. and a pressure of from 300 psig to 1000 psig, or from 400 psig to 900 psig, or from 600 psig to 800 psig, for example.
  • a de-ethenizer within a propylene production process operates at a pressure of from 350 psig to 650 psig
  • one or more embodiments of the present invention include operating the de-ethenizer at a pressure lower than that referenced.
  • one or more embodiments include operating the de-ethenizer at a pressure of less than 350 psig, or a pressure of less than 300 psig, or a pressure of less than 250 psig.
  • the fractionation system may further include a de-propenizer and a de-butenizer as known in the art.
  • the de-propenizer may receive and separate the bottoms stream (from the de-ethenizer) to form a de-propenizer overhead stream and a de-propenizer bottoms stream.
  • the de-propenizer overhead stream is composed primarily of the propylene product.
  • the de-propenizer bottoms stream generally includes the butene and C 5+ olefins.
  • the de-butenizer may receive and separate at least a portion of the de-propenizer bottoms stream to form a de-butenizer overhead stream and a de-butenizer bottoms stream.
  • the de-butenizer overhead stream is composed primarily of the recovered butene and the de-butenizer bottoms stream generally includes the C 5+ olefins.
  • at least a portion of the de-butenizer overhead stream may be recycled back to the metathesis reaction.
  • inventions described herein advantageously can reduce heating requirements in the metathesis reactor and/or the de-ethenizer, possibly by half of heating requirements for similar systems absent the embodiments of the invention.
  • embodiments described herein provide for a metathesis product stream entering the de-ethenizer having a temperature of from 50° F. to 90° F. and a pressure of from 250 psig to 350 psig, which may eliminate the need for heat exchange of the metathesis product stream.
  • FIG. 1 a simplified process flow diagram of a process 100 for producing propylene according to embodiments disclosed herein is illustrated.
  • FIG. 1 illustrates a process 100 including introducing a metathesis feed stream 102 to a metathesis reactor 104 having metathesis catalyst 105 (and optional isomerization catalyst—not shown) disposed therein to form metathesis product stream 106 including propylene, ethylene, butene and C 5+ olefins.
  • FIG. 1 illustrates a specific embodiment wherein ethylene is mixed with the metathesis feed stream 102 via line 108 ; however, it is contemplated that the ethylene may contact the metathesis feed stream via processes known in the art.
  • the metathesis product stream 106 is passed to a de-ethenizer 110 to separate at least a portion of the ethylene from the metathesis product stream 106 to form an overhead stream 112 and a bottoms stream 114 including propylene and C 4+ olefins.
  • Fresh ethylene is introduced to the de-ethenizer 110 as reflux supplement (in the same manner as the reflux liquid ethylene is introduced to the de-ethenizer 110 ) via line 116 .
  • the overhead stream 112 is passed through a partial condenser 118 to form a recycle ethylene stream 120 and a reflux liquid stream 122 .
  • the recycle ethylene stream 120 is withdrawn from the partial condenser 118 as a vapor and is compressed in compressor 128 and then recycled to the metathesis reactor 104 via line 130 .
  • the reflux liquid stream 122 is returned to the de-ethenizer 110 .
  • the overhead stream 112 may be compressed within the compressor 128 prior to passing through the partial condenser 118 , resulting in a higher condensing temperature than that shown in FIG. 1 .
  • the de-ethenizer bottoms stream 114 may be passed through a re-boiler (not shown) and returned to the de-ethenizer 110 or further separated in additional separation columns (not shown).
  • compositions and methods are described in terms of “comprising,” “containing,” or “including” various components or steps, the compositions and methods can also “consist essentially of” or “consist of” the various components and steps. All numbers and ranges disclosed above may vary by some amount. Whenever a numerical range with a lower limit and an upper limit is disclosed, any number and any included range falling within the range are specifically disclosed.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
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  • Oil, Petroleum & Natural Gas (AREA)
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US13/738,685 2013-01-10 2013-01-10 Ethylene separation process Active 2033-03-02 US9688591B2 (en)

Priority Applications (12)

Application Number Priority Date Filing Date Title
US13/738,685 US9688591B2 (en) 2013-01-10 2013-01-10 Ethylene separation process
KR1020157020376A KR101791760B1 (ko) 2013-01-10 2014-01-08 에틸렌 분리공정
CN201480003719.9A CN104918903A (zh) 2013-01-10 2014-01-08 乙烯分离方法
PCT/US2014/010631 WO2014110102A1 (fr) 2013-01-10 2014-01-08 Procédé de séparation d'éthylène
BR112015015460-3A BR112015015460B1 (pt) 2013-01-10 2014-01-08 processo de separação de etileno e processo para produzir propileno
EP14738270.9A EP2943453B1 (fr) 2013-01-10 2014-01-08 Procédé de séparation d'éthylène
MX2015008359A MX364862B (es) 2013-01-10 2014-01-08 Proceso de separacion del etileno.
CA2896614A CA2896614C (fr) 2013-01-10 2014-01-08 Procede de separation d'ethylene a desethaniseur a pression reduite
SG11201504150RA SG11201504150RA (en) 2013-01-10 2014-01-08 Ethylene separation process
MYPI2015701766A MY170494A (en) 2013-01-10 2014-01-08 Ethylene separation process
RU2015130732A RU2609014C2 (ru) 2013-01-10 2014-01-08 Способ выделения этилена
SA515360681A SA515360681B1 (ar) 2013-01-10 2015-06-25 عملية لفصل الإيثيلين

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US13/738,685 US9688591B2 (en) 2013-01-10 2013-01-10 Ethylene separation process

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US20140194664A1 US20140194664A1 (en) 2014-07-10
US9688591B2 true US9688591B2 (en) 2017-06-27

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US (1) US9688591B2 (fr)
EP (1) EP2943453B1 (fr)
KR (1) KR101791760B1 (fr)
CN (1) CN104918903A (fr)
BR (1) BR112015015460B1 (fr)
CA (1) CA2896614C (fr)
MX (1) MX364862B (fr)
MY (1) MY170494A (fr)
RU (1) RU2609014C2 (fr)
SA (1) SA515360681B1 (fr)
SG (1) SG11201504150RA (fr)
WO (1) WO2014110102A1 (fr)

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CA2860773C (fr) 2012-01-13 2020-11-03 Siluria Technologies, Inc. Procede de separation de composes hydrocarbones
US9670113B2 (en) 2012-07-09 2017-06-06 Siluria Technologies, Inc. Natural gas processing and systems
CA2893948C (fr) 2012-12-07 2022-12-06 Siluria Technologies, Inc. Procedes et systemes integres pour la conversion du methane en ethylene et la conversion de l'ethylene en produits a teneur accrue en hydrocarbures
WO2015081122A2 (fr) 2013-11-27 2015-06-04 Siluria Technologies, Inc. Réacteurs et systèmes destinés au couplage oxydatif du méthane
CA2935937A1 (fr) 2014-01-08 2015-07-16 Siluria Technologies, Inc. Systemes et procedes de conversion d'ethylene en liquides
AU2015204709B2 (en) 2014-01-09 2019-08-15 Lummus Technology Llc Oxidative coupling of methane implementations for olefin production
US10377682B2 (en) 2014-01-09 2019-08-13 Siluria Technologies, Inc. Reactors and systems for oxidative coupling of methane
US9334204B1 (en) 2015-03-17 2016-05-10 Siluria Technologies, Inc. Efficient oxidative coupling of methane processes and systems
US10793490B2 (en) 2015-03-17 2020-10-06 Lummus Technology Llc Oxidative coupling of methane methods and systems
US20160289143A1 (en) 2015-04-01 2016-10-06 Siluria Technologies, Inc. Advanced oxidative coupling of methane
US9328297B1 (en) 2015-06-16 2016-05-03 Siluria Technologies, Inc. Ethylene-to-liquids systems and methods
WO2017065947A1 (fr) 2015-10-16 2017-04-20 Siluria Technologies, Inc. Procédés de séparation et systèmes de couplage oxydatif du méthane
CA3019396A1 (fr) 2016-04-13 2017-10-19 Siluria Technologies, Inc. Couplage oxydant de methane pour la production d'olefines
US20180169561A1 (en) 2016-12-19 2018-06-21 Siluria Technologies, Inc. Methods and systems for performing chemical separations
RU2764097C2 (ru) 2017-05-23 2022-01-13 Люммус Текнолоджи Ллс Интеграция окислительного сочетания в метановые установки
KR20200051583A (ko) 2017-07-07 2020-05-13 루머스 테크놀로지 엘엘씨 메탄의 산화적 커플링를 위한 시스템 및 방법
KR102298756B1 (ko) * 2019-09-16 2021-09-03 한화토탈 주식회사 흡착분리 및 올레핀 전환 공정을 결합한 프로필렌 제조방법
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CA2896614C (fr) 2018-07-24
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MY170494A (en) 2019-08-08
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US20140194664A1 (en) 2014-07-10
KR101791760B1 (ko) 2017-11-20
SA515360681B1 (ar) 2018-01-11
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MX364862B (es) 2019-05-09
CN104918903A (zh) 2015-09-16
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